Catalyst technique



lMarch 4, 1947.

M. H ARVEsoN CATALYST TECHNIQUE Filed nec. 51. 1940 Y 2 SheetsSheet l QNNNW .NSSN

March 4, 1947. M. HQARvEsQN 20416329 CATALYST TECHNIQUE Filed Dec. 31, 1940 2 Sheets-Sheet 2 Nik Mmmm mmm alyst.

Patented Mar'. 4, 1947 UNITED STATES PATENT OFFICE cA'rALYs'r TECHNIQUE Maurice H. Arveson, Flossmoor, Ill., assigner to Standard Oil `Company, Chicago, Ill., a corporation of Indiana A-ppllcation'DecemberBl, 1940, Serial No. 372,518

3 Claims. 1

This invention relates to the contacting of fluids process and apparatus for controlling the regene eration of catalysts. l Finely divided and granular catalysts are commonly regenerated by contacting them at elevated temperatures with hot `2 concentration of the solids may be independent of the direction of ow of the gases or vapors.

This effect is caused by the phenomenon of Y hindered settling, a term used to describe the increase inv catalyst concentration in the upflow chamber resulting from the eiect of gravity on the catalyst particles causing them to settley against the upowing stream in the chamber.

" Complete settling and separation of the catalyst regeneration gases to remove carbonaceous and other deposits which lower the activity of the cat- This oxidation reaction is highly exothermic and the temperature tends to rise to levels injurious to the catalysts used. However, when the regeneration is carried out under proper conditions and excessive temperatures are avoided the catalyst can be recycled in the system almost.

indefinitely,

One object of the present invention is to control the temperature of regeneration of catalysts. Another object is to increase the life of a given catalyst. A still further lobject is to provide a method and means for utilizing the catalyst and heat more fully and t greater advantage than theyhave been in any previous catalytic system. Other objects, advantages anduses will become apparent as thedescription of the invention proceeds.

In practicing my invention I prefer toA employ the so-called fluid catalyst system wherein a pow-4 dered, granular, or pelleted solid catalyst is sus pended in reaction vapors during the conversion step, is then separated from conversion products, is next regenerated while suspended in a regeneration gas and is inally returned for effecting further reaction.

In a system ofy this kind, however, the concentration ofthe catalyst in the vapors in the reaction zone or the gases in the regenerator is not the same as the concentration at which the catalyst is introduced into the uplow chamber. Ordinarily the gases 0r vapors travel from a point near the bottom to a point near the top of the upiiow zone. The concentration of catalyst in the reactor or regenerator is always higher and under certain conditions very substantially higher than would be calculated from the rate at which l)the catalyst is introduced. In fact, there are certain conditions of low velocity in the upowing vapors or gases in the reactor or regenerator where the concentration of catalyst is nearly independent of the rate at which the catalyst is introduced. The direction of flow as well as the from the vapors, however, is prevented or hindered by the disturbing and buoying action of the upflowing stream.

j' The physical form of the catalyst in suspended catalyst conversion operations is usually a powder ranging in grade from 30 mesh to 300 mesh or finer, e. g., 100 mesh. Even coarser material has been employed and generally material falling within the range of t0 300 mesh is very satisfactory. Such a powder in compacted form has a density of about .7, i. e., it weighsl about 40 to 45 pounds per cubic foot. When aerated at a gas velocity of about 0.03 to,.2 feet per second, the catalyst becomes fluent and may have a density of about 20 to 40 pounds per cubic foot. At gas or vapor velocities of about .3 to 3 feet per second, preferably about vl to2 feet per second, the catalyst density may be about 10 to 20 pounds per `cubic -fo'ot and I prefer to employ such catalyst density in my reaction and regeneration zones.

Various means have vbeen proposed for pressuring the catalyst to be transferred to the upilow chamber. According to my invention, however, I prefer to use a powdered catalyst standpipe or catastat comprising an elongated storage or accumulation zone which can be aerated by -the introductionof inert gas when necessary to separator and passed by gravity through a stripper zone into the top of the catastat." The introduction of the catalyst from the catastat.l to theupilow chamber can be controlled by a ro-` tating valve, for example a star feeder, or other, Likewise other means automatic feeding device. of pressuring the catalyst, for example a screw pump, can be used.

The objects of my invention are attained by cooling part of the regenerated catalyst separately4` faccumulated, in a catastat for example, and recycling the cooled regenerated catalyst with the'spent catalyst to control the temperature of regeneration. Such cooling of the catalyst can be achieved by a numberk of ways but I prefer 'to effect it by heat transfer between the hot regenerated catalyst and fresh feed. If desired an l inert material of such particle size or density as to be readily removed from the regenerated gascatalyst mixture leaving the regeneration zone can be cooled in a` jacketed standpipe or catastat and circulated through the regeneration zone with the spent catalyst ,to control the temperature.

atively short residence times and high linear vapor velocities.

, Likewise part ofthe spent catalyst can be cooled y and introduced into the regenerator along with the hot spent catalyst for temperature control.

The invention is applicable broadly to catalytic hydrocarbon conversions and is described below without reference to the particular conditions of the conversion operation. Two illustrativeoperationsusing my catalyst technique, i. e.v catalytic` ample sorption media, can be regenerated or re 'vvived by my process. f

Heavy hydrocarbons such as gas oil and vaporizable hydrocarbon oils in general can be converted into gasoline with yields of about 30v to 60% per pass by vaporizing the oils and contact-` ing the vapors with nelyy divided solid catalytic materials in suspension at temperatures within the conversion range, usually of the order of betweenabout 800 and 10009 F. Various catalysts canbe used. It is preferred, however, to employ The process and apparatus described hereinafter can be adapted for the dehydrogenation of parain hydrocarbons by introducing hydrogen by line 15, for example. The hydrogen can be recovered from the fractionating system and recycled by suitable ,lines and compressors not shown. l

Suitable catalysts for the dehydrogenation are oxides of chromium, molybdenum, and/or vanadium supported on alumina. The catalyst conf centration in the'reactor ordinarily is of the or- `der of between 10 and 15 pounds per cubic foot.

A space velocity of 0.04 to 10 volumes of oil per hour per volume of catalyst within the reactor at any instant (measured at-rest in compacted 'condition regardless of degree of dispersion in use) and a catalyst residence time of 1 minute to 3{60 minutes can be used. One to sixteen mols of hydrogen per mol of feed and a hydrogen partial pressure of 30 to -450 pounds per square inch are employed. An example of the operating conditions with one of the above catalysts is a space velocity of 0.6, a catalyst residence time of minutes, a pressure of 200 pounds hydrogen partial pressure and a mol of hydrogen tomols of feed ratio of 2.

My invention is illustrated by drawings which form a part of this specification and which show diagrammatically an apparatus for carrying out the process. Referring to Figure 1 of the drawing, the feed stock is introduced through line I0 by pump II to pipe still I2 wherein the oil is vaporized and heated. Part or all of the fresh feed can be passed by line I3 in heat exchange with thehot regenerated catalyst in catastat solid refractory cracking catalysts of the metal oxide type such as silica-alumina, silica-magnesia, alumina-zirconia, silica-zirconia-alumina,

silica gel promoted vwith metal oxides adsorbed thereon, for example' magnesia and/or alumina, acid treated bentonite and other acid treated clays, for, example Super Fltrol, and other natural and synthetic catalysts of the solid metal oxide type.

`A pressure of between 0 and 50 .pounds per square inch gauge and a holding time, i. e. the average residence time of the catalyst within the reactor, of between about 0.5 and'60 minutes, for example about 5 minutes, can be used. A

space velocity, i. e. volume of liquid oil per volume of catalyst per hour, of between about 1 and 20, for example a space velocity of about 5 can be used. The volume of catalyst is the volume occupied by the catalyst present in the reactor at any one instant measured at rest orl in the pelleted condition. It is contemplated that high space'velocities will be used with low holding times, these and other conditions being combined to give the desired degree of cracking.

Catalyst, activity varies considerably and in general those catalysts which have very high ini-` tial activityand drop oi inactivity. rapidly should be operated at short catalyst 'residence As the heated vapor passes through transfer line I5 it picks up powdered catalyst from standf pipe or catastat I6. The catalyst is introduced into. the transfer line in amounts regulated by slide valve or star feeder'll. It should be understood, of course, that steam or a mechanical screw or any other suitable 'means can be used for introducingvthe catalyst into transfer line I5 and that the catalyst is carried by the vapors in this line to upflow reactor I8. If desired, the catalyst can be injected directly into the reactor lnsliead of being introduced into the transfer line Reactor. I8 can be a cylindrical vessel with a conical inlet and outlet respectively and of such size and cross-sectional area as to retain the necessary amount of catalyst for effecting the dcsired amount of conversion. The cross-sectional area should be such as to insure a vertical vapor velocity of between about' .3 and 3 feet per second in the reactor if the reaction is to be effected under the desired fluid phase conditions. It should be understood, however, that my invention is not limited tol any particular reactor size and shape and that it is only necessary to provide a contact of the vapors with a sulcient amount of catalyst to eiect the desired conversion. y

Vapors together with suspended catalyst leave the top of reactor IB through line I9 and are con# ducted to cyclone separator 20. The catalyst separated lfrom vapors in separator 20 falls into hopper or stripper 2| which in turn discharges the catalyst into standpipe or catastat 22. This standpipe is aerated by means of an inert gas such as steam introduced through line 23 and additional gasv can be introduced through line 24 for maintaining desired aeration or stripping in through line 25 to line25 which is the line conveying reaction vapors from separator 20 to further catalyst separators (not shwn) if required and thence to bubble tower 21.

Gasoline and gases are taken overhead from tower 21 through line 28 and cooler 29 to reflux drum 30. Gas canv be vented Afrom this receiver through line 3|. A portion of the liquids can be recycled by valved line 32 and pump 33 as redux in tower 21. The balancev of the liquid is conducted by valved line 34 to stabilizer 35.

Gas oil from bubble tower 21 is withdrawn by valved line 35 and all or a portion recycled. For example, the gas oil can be subjected to solvent extraction and the ramnate recycled with fresh feed.

Stabilizer 35 is operated at an elevated pressure in the conventional manner. and reboiling are controlled to take stabilized gasoline oif the base of tower 35 through valved line 31 for further treatment, storage, or use.

Gases "eliminated in producing stabilized gaso-` line pass overhead from stabilizer 35 to condenser 38 by line 39 and thence to reflux drum 40 from which -gases can be vented through line 4|. The condensate is removed from the base of redux drum 40 by means of valved line 42 and pump 43. A portion of it is returned to stabilizer 35 as reflux through valved line 44 and the rest of the condensate is Withdrawn from the system by valved line 45. l

Spent catalyst from catastat 22 is introduced through valve or star feeder 46 by means of an oxygen-containing gas such as air from line 41 into line 4B and conveyed therein to upiiow regenerator 49. The regenerator can be a cylindrical vessel similar in size and shape to reactor I8 since I prefer to burn the carbonaceous deposit from the catalyst while the catalyst is in the suspended dense phase condition that is obtainable with the use of vertical vapor velocities of about 1 or 2 feet per second.

.When the regeneration is carried out under proper conditions and excessive temperatures are avoided the catalyst can be recycled in the system almost indefinitely. The temperatures employed in regeneration` ordinarily are about 1000 F. to

1200 for example, below about l050 F. Higher temperatures can be used with certain oxide catalysts whereas lower temperatures are sometimes required with activated natural clays, magnesia and the like.

The regeneration is highly exothermic and the temperature tends to rise to levels injurious to the activity of the catalyst. Regeneration temperatures, however, can be held within close limits by recycling cool regenerated catalyst from standpipe I4. Cool catalyst from catastat |4 can be introduced through valve or star feeder 50 by means of an oxygen-containing gas such as air from line into line 48'and passed in controlled amounts to upfiow regenerator 49 with spent catalyst from catastat 22.v

Regenerated catalyst is carried out of the top of regeneratorl 49 through line 52 to cyclone separator 53. The regeneration gasesand catalyst separated from some of the catalyst in separator 53 are withdrawn through line 54 to separator 55. The regeneration gases separated from the catalyst-in separator 55 are withdrawn through line 55, and both heat and catalyst can be recovered therefrom in any conventional manner. If desired the separators 53 and 55 can be combined Reflux, pressure. f

` stripper 2|. Gases from stripper 2| are vented and the separated catalyst stream divided between catastats I4 and I5.

Catalyst from separator 53 falls to stripper 51 and thence to standpipe or catastat I4. Aerating gas is introduced through lines 58 and55 and such gas is preferably withdrawn from the top of stripper51 through line 5 0 and conducted to line 54. Likewise catalyst recovered in separator 55 falls to hopper 5| and thence to standpipe I5.

Aerating gas is introduced through lines 52 and 53 and the gases vented from the topA of hopper 5| and separator 55 through lines 54 and 55 respectively.

Reverting to standpipe I4, it is provided with cooler designated generally by the numeral 55 which for example can take the form illustrated in Figures 2, 3 and 4. As to the material to be used to furnish cooling, the preferred ymaterial is fresh feed to the unit which can be passed countercurrent to the descending hotl aerated catalyst. 'I'hus the fresh feed is preheated very close to reaction temperature. When the reaction temperature is attained the furnace I2 can be used only to start up the unit. .The fresh feed enters the cooler 65 by valved line I3, leaves the exchanger byline 55, and passes by either of valved lines |0 and 51 to furnace I2 or transfer line I5, respectively. Alternatively, water can be introduced Ato cooler 65 and converted into steam; steam can be introduced and superheated, or molten salt canbe introduced and the heat taken up by the molten salt used in turn to generate steam. Also the fresh feed and hot catalyst can be heat exchanged indirectly by molten salt extent of heat exchange within a given section. I

Such an apparatus is illustrated ln Figure 3.

Referring to Figure 2, the standpipe I4 can be a central tube and the cooling of the standpipe effected by a liquid being passed through the annulus 58 between the standpipe I4 and the shell 59, the flow being countercurrent. It is preferred that the cooler comprises units of dual tube, single pass heat exchangers.' in series or parallel with by-passing of a given unit possible. Conventional means such as elbows 10 can be used to connect the units.

The modification of my cooler illustrated in Figure 3 comprises one or more pipes I4 for the downward ow of catalyst and one or more pipes 1| for the upward flow of the cooling material are encased in a single shell 12. can be filled with a solid or liquid heat-transferring medium, for example, solid aluminum, which can be melted and removed for repair purposes or to regulate the extent of heat'transfer. Molten salt,1ead or other liquid medium can be used whereby the level can be adjusted to oadjust the extent of heat transfer,

can contain helical fins 13 to impart a spiral motion to the upiiowing oil or other heat exchange medium within shell 'I4 whereby an effective heat exchange is attained.

Various other modifications of the invention will be apparent to those skilled in the art from the above description and I do not limit myself to any ofthe details hereinabove set forth except as defined by the following claims.

I claim:

1. In apparatus for the regeneration of catalyst, the combination of an elongated contacting chamber of substantial cross-sectional area, inlet means at a low point in said 'contacting chamber, an outlet for the elongated chamber com- The shell 'I2Y immicatin'g with a catalyst-separating means, a standpipe outside said .contacting chamber, al conduit from said separating means to the top 4of 1 said standpipe, valve means for withdrawing catalyst from the bottom of said standpipe, a shell around at least a portion of the length of said 1 standpipe, inlet means for supplying a heat trans- ,1 fermedium to said shell, an'outlet means for withdrawingv heat transfer medium from saidv shell, and a regeneration gas line extending between the bottom of saidstandpipe and said conn tactlng chamber and adapted to transfer catalyst l from said standpipe to said chamber.

2. In i catalytic `conversion process wherein i catalyst is regenerated while suspended in regen- 1 eration gas in aregeneration zone and wherein l critical regeneration4 gas velocities are requiredf for maintaining said suspended catalyst in dense phase condition, the method of operation whichl l comprises separating hot regenerated catalyst from regeneration gas, accumulating at least a portion of the separated catalyst at the top of a dense column of laerated regenerated catalyst,

t surrounding Said regenerated catalyst column l witha. heat exchange fluid whereby the catalyst is cooled as it moves downwardly in said column,

maintaining thel column 'at such height and atv such density that the pseudo-hydrostatic pressure 1 at its base exceeds the pressure of a regeneration gas stream communicating with the/ibase of said fcolumn and entering the base of said regeneration zone, dispersing cooled regenerated catalyst from the base o! the column into said stream and carf rying said dispersed catalyst by said stream back to said regeneration zone, the dispersion of the catalyst in the stream and its return to the r'egeneration zone being effected by utilizing the pseudo hydrostatic pressure exerted by said dense column of aerated regenerated catalyst.

3. The process of claim 2 wherein the heat exchange uid comprises at least a part of the charging stock to said catalytic conversion process.

MAURICE H. ARVESON.

REFERENCES CITED The following references are of record in the' le of this patent:

UNITED STATES PATENTS Marancik et al Sept. 22, 1942 

